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EP0842385B2 - Method and device for the production of variable amounts of a pressurized gaseous product - Google Patents
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EP0842385B2 - Method and device for the production of variable amounts of a pressurized gaseous product - Google Patents

Method and device for the production of variable amounts of a pressurized gaseous product Download PDF

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Publication number
EP0842385B2
EP0842385B2 EP96927545A EP96927545A EP0842385B2 EP 0842385 B2 EP0842385 B2 EP 0842385B2 EP 96927545 A EP96927545 A EP 96927545A EP 96927545 A EP96927545 A EP 96927545A EP 0842385 B2 EP0842385 B2 EP 0842385B2
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EP
European Patent Office
Prior art keywords
liquid fraction
heat exchanger
heat
liquid
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP96927545A
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German (de)
French (fr)
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EP0842385B1 (en
EP0842385A1 (en
Inventor
Horst Corduan
Horst Altmeyer
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Linde GmbH
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Linde GmbH
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Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0842385A1 publication Critical patent/EP0842385A1/en
Publication of EP0842385B1 publication Critical patent/EP0842385B1/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the invention relates to a method and a device for the variable production of a gaseous printed product by low-temperature separation of air by increasing the pressure in the liquid state and subsequent Evaporation.
  • the invention is therefore based on the object of specifying a method and a device which, if possible can be operated flexibly and in particular avoid the disadvantages described above.
  • the gaseous print product is obtained in liquid form from the or one of the rectification columns removed and buffered in a first storage tank.
  • the liquid level in the tank increases or decreases.
  • the amount of liquid fraction produced in the rectification that is not currently evaporating or otherwise can be introduced into the tank; accordingly if there is a high product requirement, liquid is evacuated from the tank.
  • “Storage tank” here means any device for storing liquid. there it can be, for example, an external tank with its own insulation, but also a different type of vessel, which is arranged within the cryogenic separation plant and suitable for buffering liquid is.
  • Any known method can be used to increase the pressure in the liquid state, for example Pressure build-up evaporation at the storage tank, utilization of a static height, pumps upstream or downstream the storage tank, or combinations of these methods.
  • the liquid fraction is preferably passed through pressurized a pump located downstream of the tank. The throughput of this pump can be controlled to cause variation in the amount of product.
  • the inventive method also has a refrigeration cycle with a cycle compressor and a relaxation machine.
  • a heat carrier in particular a process gas for air separation, is compressed therein, Relieved of work and returned to the circuit compressor.
  • This cycle Cold generated to compensate for insulation and exchange losses and possibly for product liquefaction.
  • the circuit compressor also serves to compress the heat carrier, which is against the one to be evaporated Product is condensed and buffered in a second storage tank (first partial flow of the heat transfer medium). It condenses the heat transfer medium to a pressure that corresponds to a condensation temperature that is at least approximately the same is the evaporation temperature of the liquid pressurized fraction. At least part of the in the rotary compressor compressed heat transfer medium is returned to the circuit compressor, in particular the second partial flow after his work relaxation or part of it. The second partial flow of the compressed in the circuit compressor The heat transfer medium does not need to be discarded or not at all, but at least becomes partially in a circle. Refrigeration cycle and variable product evaporation are integrated in the invention; the same The machine is used both for the generation of cold and for the production of the vaporization of the liquid fraction required pressure.
  • the first partial flow in the invention also corresponds to the variable product quantity varied.
  • this variation can be implemented in different ways and thus flexibly to the current one Needs to be adjusted.
  • the amount of heat carrier compressed in the circuit compressor is kept constant when there is an increased need for gaseous pressure product.
  • the variation of the first partial flow is absorbed by a corresponding variation of the second partial flow of the heat transfer medium.
  • the amount of the second partial flow is decreased / increased by the same amount by which the amount of the first partial flow is increased / decreased.
  • An increased amount of heat transfer medium liquefied in the second partial flow is temporarily stored in the second tank; an increased amount of gas in the second partial flow can be compensated for by a corresponding removal of gas (for example as a product) from the circuit; Conversely, if the production is below average, a correspondingly smaller amount of gas is withdrawn from the circuit.
  • the system can be operated in a second mode of operation.
  • the throughput remains of the second partial flow is the same, while the variation of the first partial flow is followed by the circuit compressor. If there is an increased need for gaseous pressure product, the amount of the second partial stream is kept constant and the amount of heat carrier compressed in the circuit compressor by the same amount as the amount of the first Partial flow increased. Nevertheless, in the method according to the invention, the relative ones are also in this operating mode Fluctuations in the compressor throughput are comparatively small since the circulating volume can remain constant. The constant proportion of the gas compressed in the circulation compressor dampens the relative deflections of the compressor throughput.
  • the two modes of operation can also be combined by the fluctuations of the first partial flow partly by varying the second partial flow and partly by changing the throughput be compensated on the circuit compressor. If there is an increased need for gaseous printed product, then both the amount of the heat carrier compressed in the circuit compressor and the amount of the second partial stream are increased reduced.
  • the rectification system has a double column consisting of a pressure column and a low pressure column
  • the amount of additional current that is supplied to the work-relieving relaxation can be reduced if there is an increased need for gaseous printed product and at least an excess of cold partially compensated.
  • the work-performing relaxation of the further current leads approximately to the inlet pressure of the circuit compressor (lower level of the refrigeration circuit) to about atmospheric pressure and the more power that is relaxed during work is drawn off as an unpressurized gas product.
  • This also allows fluctuations the amount of gas circulating in the circuit.
  • the first mode of operation by reducing the amount of the second partial flow a corresponding reduction in the amount of work-relaxed additional current can be compensated.
  • the second mode of operation constant throughput during the work relieving pressure of the second partial flow
  • an increase in the circulation compressor throughput can be compensated for by a reduction in the amount of gas that leaves the cycle as another stream.
  • any process stream available in the process can act as a heat transfer medium for the refrigeration cycle and the evaporation of the liquid fraction can be used, for example air or another oxygen-nitrogen mixture.
  • nitrogen from the rectification system is preferably used as the heat carrier, in the case a double column, for example gaseous nitrogen, which accumulates at the top of the pressure column.
  • the entire cycle nitrogen is produced in the plant itself.
  • a subset of the heat transfer medium come from an external source, for example by feeding liquid nitrogen from another plant or from a tank truck to the second storage tank.
  • the second storage tank can act in addition to its buffering effect for variable print product production also as a safety reserve (backup) for a temporary failure of the system and / or used as a buffer for liquid product.
  • the use of nitrogen as a heat transfer medium has the advantage that the refrigeration cycle and evaporation of the printed product does not have any negative effects on the rectification, as is the case when feeding in against Print product liquefied air and when feeding gaseous air from a relaxation machine in a low pressure column would be the case.
  • the rectification can thus be used in the method according to the invention optimally driven by nitrogen as a heat transfer medium.
  • the process is therefore also for high product purities and - exploit suitable, as well as for the extraction of argon after the air separation in the narrower sense (e.g. raw argon column connected to the low pressure column of a double column).
  • the main heat exchanger system has a heat exchanger block has in which both the cooling of the feed air and the evaporation of the liquid fraction below increased pressure.
  • the main heat exchanger system has a plurality of heat exchanger blocks has, in particular a first and a second heat exchanger block, wherein in the first heat exchanger block the cooling of the feed air and in the second heat exchanger block the evaporation of the liquid Fraction is carried out under increased pressure.
  • the two heat exchanger blocks are coupled by a compensating current that one of the two heat exchanger blocks between the removed warm and cold end and the other of the two heat exchanger blocks between the warm and cold end is fed.
  • the invention also relates to a device according to claim 7.
  • Compressed and cleaned feed air 10 is under a pressure of 5 to 10 bar, preferably 5.5 to 6.5 bar cooled in the heat exchanger 11, which forms the main heat exchanger system with the heat exchanger 12. about Line 13, it is introduced into a pressure column 14 at about dew point temperature.
  • the pressure column belongs to that Rectification system, which also has a low pressure column 15, preferably at a pressure of 1.3 to 2 bar 1.5 to 1.7 bar is operated. Pressure column 14 and low pressure column 15 are via a main condenser 16 thermally coupled.
  • Bottom liquid 17 from the pressure column 14 is in a counterflow 18 against product flows of the low pressure column supercooled and fed into the low pressure column 15 (line 19).
  • Gaseous nitrogen 20 from the head the pressure column 14 is in the main condenser 16 against evaporating liquid in the sump of the low pressure column 15 liquefied.
  • the condensate 21 is partly fed as a return to the pressure column 14 (line 22) and to another part 23 introduced after supercooling 18 in a separator 25 (24).
  • the low pressure column 15 will from the separator 25 supplied with return liquid (line 26).
  • Low pressure nitrogen 27 and impure nitrogen 28 are 15 in after removal from the low pressure column the heat exchangers 18 and 11 warmed to about ambient temperature.
  • the impure nitrogen 30 can be used for regeneration a molecular sieve, not shown, can be used for air purification; the low pressure nitrogen 29 is either discharged as a product or used in an evaporative cooler to cool cooling water.
  • Oxygen is withdrawn as a liquid fraction via line 31 from the bottom of the low-pressure column 15, supercooled (18) and introduced (32) into a liquid oxygen tank (first storage tank) 33.
  • the liquid oxygen tank 33 is preferably at about atmospheric pressure.
  • Liquid oxygen 34 from the first storage tank 33 is brought to an increased pressure of, for example, 5 to 80 bar by means of a pump 35, depending on what is required Product printing. (Of course, other methods for increasing the pressure in the liquid phase can also be used, for example by utilizing a hydrostatic potential or by pressure build-up evaporation on one Storage tank.)
  • the liquid high pressure oxygen 36 is evaporated in the heat exchanger 12 and as internally compressed deducted gaseous product 37.
  • the part of the gaseous nitrogen from the pressure column 14 that is not fed to the main condenser 16 is withdrawn via lines 38, 39 and 40 through the heat exchanger 11 and one as a heat carrier Refrigeration circuit supplied, which, among other things, a two-stage circuit compressor 41, 42 and an expansion turbine 43 includes.
  • the nitrogen is compressed from about pressure stage pressure to a pressure which corresponds to a nitrogen condensation temperature which is at least approximately equal to the evaporation temperature r of the liquid pressurized oxygen 36. This pressure is - depending on the given delivery pressure of the oxygen - For example 15 to 60 bar.
  • a first partial flow 45 of the highly compressed nitrogen 44 is against the evaporating Oxygen 36 at least partially, preferably completely or substantially completely liquefied and fed into a separator 46.
  • the second partial flow 59 of the nitrogen compressed in the circuit compressor is at the high pressure and at a temperature that lies between the temperatures at the warm and cold ends of the heat exchanger 12, fed to the expansion turbine 43 and relaxed there while performing work at about pressure column pressure.
  • the relaxed one second partial flow 60 becomes partly through heat exchanger 12 (via 61, 62), partly through heat exchanger 11 (via 63, 64, 39, 40) returned to the inlet of the circuit compressor 41, 42.
  • Liquid nitrogen from the separator 46 can be fed as a return line to the pressure column 14 via line 47 and / or are introduced via line 48 into a second storage tank (liquid nitrogen tank 49) which is under a pressure of, for example, 1 to 5 bar, preferably below about atmospheric pressure.
  • the tank can also if necessary, excess liquid 50 is fed from the separator 25, which is not used as a return is required for the low pressure column 15. If necessary, liquid nitrogen can be fed into the separator by means of a pump 51 46 are pressed (line 52).
  • Part of the nitrogen 53 from line 39 can exit the heat exchanger 11 at an intermediate temperature be removed.
  • This part serves in part as equalizing flow 54, with the aid of which the efficiency of the main heat exchanger system is increased 11, 12 can be improved, and in part as a further stream 55 of the heat carrier, which in a second expansion turbine 56 is expanded to work slightly above atmospheric pressure.
  • the working relaxed further stream 57 is heated in the heat exchanger 12 to about ambient temperature and leaves the plant as a gaseous product 58.
  • Liquid oxygen and / or liquid nitrogen can be withdrawn as products from the storage tanks 33, 49 (the corresponding lines are not shown in the drawing).
  • the alternating storage has no disruptive influences on the rectification, in particular, neither liquid air is fed to the rectification nor is low-pressure air directly into the low-pressure column fed.
  • a conventional one can be located at an intermediate point 66 of the low-pressure column 15 Argon rectification connected, as indicated in the drawing by the lines shown there.
  • the first stage 41 of the cycle compressor is also used as a product compressor by between the first and the second stage a product stream 65 under a pressure of preferably 8 to 35 bar, for example, 20 bar is withdrawn.
  • the two basic operating modes of a method and a device according to the invention are now explained below.
  • the system is designed for a certain average amount of pressurized oxygen product. Production can fluctuate around this average value, and between a minimum and a maximum value. To explain how this fluctuation is achieved, the two extreme operating cases ("Max.”, "Min.”) And the operating case of the average pressure oxygen production (“Average”) of a system are presented in the following numerical examples, the 190,000 Nm 3 / h Process air processed.
  • the pressures are Pressure column 14 5.1 bar Low pressure column 15 1.3 bar Pressurized oxygen 37 26 bar Entry of the circuit compressor 4.8 bar Outlet of the circuit compressor 42 bar Liquid oxygen tank 33 1.1 bar Liquid nitrogen tank 1.1 bar
  • Table 1 relates to the mode of operation in which the expansion turbine 43 for the second partial flow 59 is operated at a constant speed; in the operating mode shown in Table 2, the throughput through the circuit compressor 41, 42 is kept constant. Of course, any transition between these two modes of operation is also possible in the exemplary embodiment.
  • the amounts of the respective currents for the three operating cases mentioned are given in 1000 Nm 3 / h.
  • the reference symbols in the first column of the table refer to the drawing. (Constant throughput by turbine 43) Max. Avg.
  • the scheme in the drawing is divided in half by a dashed line.
  • the left half essentially contains the refrigeration cycle and the storage tanks; the entire rectification is in the right half.
  • all flows in the right half of the drawing remain completely or essentially unchanged, the fluctuations in the production of pressurized oxygen only affect the circuit and the storage tanks. This is reflected in the first six lines of the two tables, in which all currents are mentioned that cross the dashed line; these have the same throughput in all operating cases, while the amount of evaporation changes (reference symbols 36, 37).
  • the second partial flow 59, 60 is kept constant.
  • the one for evaporation necessary variation of the first partial flow 45 is achieved by the corresponding change in the throughput the circulation compressor (stream 44) causes:
  • the production increases from the average the maximum value
  • the throughput through the circuit compressor increases by approximately the same amount as the product quantity to.
  • the additional gas is made available by a corresponding reduction in the amount of gas, which is taken as a further stream 55, 57, 58 through the turbine 56 from the circuit.
  • the fluctuating amounts of liquefied heat transfer medium (first partial flow 45) are buffered by that with above-average production via line 48 excess liquid to the second storage tank 49th is fed; conversely, the missing liquid is removed from the liquid nitrogen tank via line 52 with a small amount of product tracked to keep the return flow rate for the pressure column 14 constant.
  • Table 1 The numerical example of Table 1 is designed so that an average excess of liquid of 1500 Nm 3 / h oxygen and nitrogen is generated. This can be removed continuously, intermittently or in variable amounts in the form of liquid products. In addition, it is also possible with the method to change the average cooling capacity of the circuit and thus the average amount of liquid products during operation by adjusting the average speeds of the turbines accordingly.
  • the system can be operated particularly flexibly not only with regard to the internally compressed printed product, but also with regard to liquid production.

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Abstract

In the method proposed, charge air is fed to a cryogenic rectifying system (15, 16) where it is split up into its constituent gases, and a liquid fraction (31, 32) is taken off and passed into a first storage tank (33). The pressure of any suitable amount of the liquid fraction (34) is increased (35). The liquid fraction (36) is then evaporated under the increased pressure by indirect heat exchange (12) and converted into a pressurized gaseous product (37). A heat-transfer fluid circulates in a refrigeration circuit fitted with a compressor (41, 42). Part (45) of the flow of heat-transfer fluid (44) compressed in the compressor (41, 42) is fed to the indirect heat-exchange unit (12) where the liquid fraction (36) is evaporated and the heat-transfer fluid (44) at least partly liquefied. Another part (59) of the flow of heat-transfer fluid (44) compressed in the compressor (41, 42) is allowed to expand (43), doing useful work. Liquefied heat-transfer fluid (45, 48) is stored in a buffer storage tank (49).

Description

Die Erfindung betrifft ein Verfahren und eine Vorrichtung zurvariablen Erzeugung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft mittels Druckerhöhung im flüssigen Zustand und anschließender Verdampfung.The invention relates to a method and a device for the variable production of a gaseous printed product by low-temperature separation of air by increasing the pressure in the liquid state and subsequent Evaporation.

Die Methode, ein Flüssigprodukt eines Luftzerlegers auf Druck zu bringen und anschließend zu verdampfen, wird häufig auch als "Innenverdichtung" bezeichnet. Derartige Prozesse sind für die Gewinnung einer konstanten Menge eines unter Druck stehenden Gases altbekannt (beispielsweise DE-C-752439) und bieten gegenüber der gasförmigen Produktverdichtung den Vorteil geringerer Apparatekosten.The method of pressurizing a liquid product from an air separator and then evaporating it, is often referred to as "internal compression". Such processes are for obtaining a constant amount of a pressurized gas well known (for example DE-C-752439) and offer compared to the gaseous Product compaction has the advantage of lower equipment costs.

Ebenfalls bekannt sind "Wechselspeicherverfahren" mit mindestens zwei Speichertanks, bei denen variable Mengen eines Luftgases unter Atmosphärendruck gewonnen werden können und trotzdem ein stationärer Betrieb der Rektifikation möglich ist (siehe beispielsweise W. Rohde, Linde-Berichte aus Technik und Wissenschaft, 54/1984, Seiten 18 bis 20).Also known are "removable storage methods" with at least two storage tanks, in which variable Amounts of an air gas can be obtained under atmospheric pressure and still a stationary operation of the Rectification is possible (see, for example, W. Rohde, Linde Reports from Technology and Science, 54/1984, pages 18 to 20).

Die Druckschriften DE-B-1056633, EP-A-422974, EP-A-524785 und EP-A-556861 zeigen Prozesse, die Innenverdichtung und Wechselspeicherung kombinieren, indem sowohl das zu verdampfende Flüssigprodukt als auch bei der Verdampfung verflüssigter Wärmeträger (Luft oder Stickstoff) in Speichertanks gepuffert werden. Das Problem des variierenden Bedarfs an Wärmeträger für die Verdampfung des Flüssigprodukts wird in DE-B-1056633 dadurch gelöst, daß der jeweils nicht für die Verdampfung benötigte Anteil des Wärmeträgers arbeitsleistend entspannt und verworfen wird. Davon ist man später abgekommen und verdichtet statt dessen variable Mengen an Wärmeträger (EP-A-422974, EP-A-524785 und EP-A-556861). Während im ersten Fall ein gereinigtes Gas ungenutzt verlorengeht, treten im zweiten Fall große relative Schwankungen des Verdichterdurchsatzes auf. Beide Arten von Anlagen können nur in der jeweiligen Betriebsweise gefahren werden.The documents DE-B-1056633, EP-A-422974, EP-A-524785 and EP-A-556861 show processes that involve internal compression and swap storage by combining both the liquid product to be evaporated and when evaporating liquefied heat transfer media (air or nitrogen) in storage tanks. The problem of the varying need for heat transfer medium for the evaporation of the liquid product is described in DE-B-1056633 solved that the portion of the heat transfer medium not required for the evaporation relaxes work and is discarded. This was later abandoned and instead variable amounts of heat transfer medium (EP-A-422974, EP-A-524785 and EP-A-556861). While in the first case a cleaned gas is lost unused, kick in the second case there are large relative fluctuations in the compressor throughput. Both types of attachments can only be driven in the respective mode of operation.

Der Erfindung liegt daher die Aufgabe zugrunde, ein Verfahren und eine Vorrichtung anzugeben, die möglichst flexibel betrieben werden können und die insbesondere die oben beschriebenen Nachteile vermeiden.The invention is therefore based on the object of specifying a method and a device which, if possible can be operated flexibly and in particular avoid the disadvantages described above.

Diese Aufgabe wird durch das Verfahren gemäß Anspruch 1 gelöst.This object is achieved by the method according to claim 1.

Das gasförmig zu gewinnende Druckprodukt wird in flüssiger Form aus der oder einer der Rektifiziersäulen abgezogen und in einem ersten Speichertank gepuffert. Je nachdem, ob momentan eine unterdurchschnittliche oder eine überdurchschnittliche Produktmenge erzeugt wird, steigt odersinkt der Flüssigkeitsstand im Tank. Beispielsweise kann diejenige Menge an in der Rektifikation erzeugter flüssiger Fraktion, die momentan nicht verdampft oder anderweitig (beispielsweise als Flüssigprodukt) verwendet werden kann, in den Tank eingeführt werden; entsprechend wird bei hohem Produktbedarf Flüssigkeit aus dem Tank zur Verdampfung geführt. Es ist aber auch möglich, die gesamte flüssige Fraktion in den Speichertank einzuleiten und jeweils die aktuell benötigte Menge zu entnehmen und der Verdampfung zuzuführen. Unter "Speichertank" ist hier jede Vorrichtung zur Flüssigkeitsspeicherung zu verstehen. Dabei kann es sich beispielsweise um einen externen Tank mit eigener Isolierung handeln, aber auch um eine andere Art von Gefäß, das innerhalb der Tieftemperaturzerlegungsanlage angeordnet und zur Pufferung von Flüssigkeit geeignet ist.The gaseous print product is obtained in liquid form from the or one of the rectification columns removed and buffered in a first storage tank. Depending on whether it is currently below average or If an above-average amount of product is produced, the liquid level in the tank increases or decreases. For example can be the amount of liquid fraction produced in the rectification that is not currently evaporating or otherwise (for example, as a liquid product) can be introduced into the tank; accordingly if there is a high product requirement, liquid is evacuated from the tank. But it is also possible to do the whole introduce liquid fraction into the storage tank and take the currently required amount and the evaporation supply. "Storage tank" here means any device for storing liquid. there it can be, for example, an external tank with its own insulation, but also a different type of vessel, which is arranged within the cryogenic separation plant and suitable for buffering liquid is.

Zur Druckerhöhung im flüssigen Zustand kann jede bekannte Methode angewandt werden, beispielsweise Druckaufbauverdampfung am Speichertank, Ausnutzung einer statischen Höhe, Pumpen stromaufwärts oder stromabwärts des Speichertanks, oder auch Kombinationen dieser Methoden. Vorzugsweise wird die flüssige Fraktion durch eine stromabwärts des Tanks angeordnete Pumpe auf Druck gebracht. Der Durchsatz dieser Pumpe kann gesteuert werden, um die Variation der Produktmenge zu bewirken.Any known method can be used to increase the pressure in the liquid state, for example Pressure build-up evaporation at the storage tank, utilization of a static height, pumps upstream or downstream the storage tank, or combinations of these methods. The liquid fraction is preferably passed through pressurized a pump located downstream of the tank. The throughput of this pump can be controlled to cause variation in the amount of product.

Das erfindungsgemäße Verfahren weist außerdem einen Kältekreislauf mit einem Kreislaufverdichter und einer Entspannungsmaschine auf. Darin wird ein Wärmeträger, insbesondere ein Prozeßgas der Luftzerlegung, verdichtet, arbeitsleistend entspannt und wieder zum Kreislaufverdichter zurückgeführt. Mit Hilfe dieses Kreislaufs wird Kälte zum Ausgleich von Isolations- und Austauschverlusten und gegebenenfalls zur Produktverflüssigung erzeugt.The inventive method also has a refrigeration cycle with a cycle compressor and a relaxation machine. A heat carrier, in particular a process gas for air separation, is compressed therein, Relieved of work and returned to the circuit compressor. With the help of this cycle Cold generated to compensate for insulation and exchange losses and possibly for product liquefaction.

Der Kreislaufverdichter dient gleichzeitig zur Verdichtung des Wärmeträgers, der gegen das zu verdampfende Produkt kondensiert und in einem zweiten Speichertank gepuffert wird (erster Teilstrom des Wärmeträgers). Er verdichtet den Wärmeträger auf einen Druck, der einer Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur der flüssig auf Druck gebrachten Fraktion ist. Mindestens ein Teil des im Kreistaufverdichter verdichteten Wärmeträgers wird zum Kreislaufverdichter zurückgeleitet, insbesondere der zweite Teilstrom nach seiner arbeitsleistenden Entspannung oder ein Teil davon. Der zweite Teilstrom des im Kreislaufverdichter komprimierten Wärmeträgers braucht also nicht oder nicht vollständig verworfen zu werden, sondern wird mindestens teilweise im Kreis geführt. Kältekreislauf und variable Produktverdampfung sind bei der Erfindung integriert; dieselbe Maschine dient sowohl zur Kälteerzeugung als auch zur Erzeugung des für die Verdampfung der flüssigen Fraktion benötigten Drucks.The circuit compressor also serves to compress the heat carrier, which is against the one to be evaporated Product is condensed and buffered in a second storage tank (first partial flow of the heat transfer medium). It condenses the heat transfer medium to a pressure that corresponds to a condensation temperature that is at least approximately the same is the evaporation temperature of the liquid pressurized fraction. At least part of the in the rotary compressor compressed heat transfer medium is returned to the circuit compressor, in particular the second partial flow after his work relaxation or part of it. The second partial flow of the compressed in the circuit compressor The heat transfer medium does not need to be discarded or not at all, but at least becomes partially in a circle. Refrigeration cycle and variable product evaporation are integrated in the invention; the same The machine is used both for the generation of cold and for the production of the vaporization of the liquid fraction required pressure.

Selbstverständlich wird auch bei der Erfindung der erste Teilstrom entsprechend der variablen Produktmenge variiert. Diese Variation kann jedoch hier auf unterschiedliche Weise realisiert und damit flexibel an die jeweils aktuellen Bedürfnisse angepaßt werden. It goes without saying that the first partial flow in the invention also corresponds to the variable product quantity varied. However, this variation can be implemented in different ways and thus flexibly to the current one Needs to be adjusted.

In einer ersten Betriebsweise wird bei erhöhtem Bedarf an gasförmigem Druckprodukt die Menge des im Kreislaufverdichter verdichteten Wärmeträgers konstant gehalten. Die Variation des ersten Teilstroms wird durch eine entsprechende Variation des zweiten Teilstroms des Wärmeträgers aufgefangen. Bei Erhöhung/Verringerung der Produktion wird die Menge des zweiten Teilstroms um denselben Betrag verringert/erhöht, um den die Menge des ersten Teilstroms erhöht/verringert wird. (Mit "Menge" werden hier molare Mengen pro Zeiteineinheit bezeichnet, die z.B. in Nm3/h angegeben werden können.) Damit kann der Kreislaufverdichter konstant gefahren werden, beispielsweise mit seinerAuslegungskapazität, eine Steuerung in Abhängigkeit von der Produktmenge ist nicht nötig. Eine erhöhte Menge an im zweiten Teilstrom verflüssigtem Wärmeträger wird im zweiten Tank zwischengespeichert; eine erhöhte Gasmenge im zweiten Teilstrom kann durch eine entsprechende Entnahme von Gas (beispielsweise als Produkt) aus dem Kreislauf kompensiert werden; umgekehrt wird bei unterdurchschnittlicher Produktion eine entsprechend geringere Menge an Gas aus dem Kreislauf entnommen.In a first mode of operation, the amount of heat carrier compressed in the circuit compressor is kept constant when there is an increased need for gaseous pressure product. The variation of the first partial flow is absorbed by a corresponding variation of the second partial flow of the heat transfer medium. When production is increased / decreased, the amount of the second partial flow is decreased / increased by the same amount by which the amount of the first partial flow is increased / decreased. ("Quantity" here denotes molar quantities per unit of time, which can be specified, for example, in Nm 3 / h.) This means that the circuit compressor can be operated constantly, for example with its design capacity, and control depending on the quantity of product is not necessary. An increased amount of heat transfer medium liquefied in the second partial flow is temporarily stored in the second tank; an increased amount of gas in the second partial flow can be compensated for by a corresponding removal of gas (for example as a product) from the circuit; Conversely, if the production is below average, a correspondingly smaller amount of gas is withdrawn from the circuit.

Alternativ dazu kann die Anlage in einerzweiten Betriebsweise gefahren werden. Dabei bleibt der Durchsatz des zweiten Teilstroms gleich, während die Variation des ersten Teilstroms vom Kreislaufverdichter nachgefahren wird. Bei erhöhtem Bedarf an gasförmigem Druckprodukt wird also die Menge des zweiten Teilstroms konstant gehalten und die Menge des im Kreislaufverdichter verdichteten Wärmeträgers um denselben Betrag wie die Menge des ersten Teilstroms erhöht. Dennoch sind beim erfindungsgemäßen Verfahren auch bei dieser Betriebsweise die relativen Schwankungen des Verdichterdurchsatzes vergleichweise gering, da die Kreislaufmenge konstant bleiben kann. Der gleichbleibende Anteil des im Kreislaufverdichter komprimierten Gases dämpft die relativen Ausschläge des Verdichterdurchsatzes.Alternatively, the system can be operated in a second mode of operation. The throughput remains of the second partial flow is the same, while the variation of the first partial flow is followed by the circuit compressor. If there is an increased need for gaseous pressure product, the amount of the second partial stream is kept constant and the amount of heat carrier compressed in the circuit compressor by the same amount as the amount of the first Partial flow increased. Nevertheless, in the method according to the invention, the relative ones are also in this operating mode Fluctuations in the compressor throughput are comparatively small since the circulating volume can remain constant. The constant proportion of the gas compressed in the circulation compressor dampens the relative deflections of the compressor throughput.

Die beiden Betriebsweisen können aber auch kombiniert werden, indem die Schwankungen des ersten Teilstroms zu einem Teil durch Variation des zweiten Teilstroms und zu einem anderen Teil durch Veränderung des Durchsatzes am Kreislaufverdichter kompensiert werden. Bei erhöhtem Bedarf an gasförmigem Druckprodukt werden dann sowohl die Menge des im Kreislaufverdichterverdichteten Wärmeträgers erhöht als auch die Menge des zweiten Teilstroms verringert.However, the two modes of operation can also be combined by the fluctuations of the first partial flow partly by varying the second partial flow and partly by changing the throughput be compensated on the circuit compressor. If there is an increased need for gaseous printed product, then both the amount of the heat carrier compressed in the circuit compressor and the amount of the second partial stream are increased reduced.

Je nach Bedarf kann zwischen diesen Betriebsweisen gewechselt werden, beispielsweise um Flüssigproduktentnahmen aus dem Tank zu kompensieren oder für bestimmte Zeit eine erhöhte Menge an Flüssigprodukt(en) zu liefern. Je nach Menge des zweiten Teilstroms wird bei dessen arbeitsleistender Entspannung unterschiedlich viel Kälte erzeugt.Depending on your needs, you can switch between these modes of operation, for example to withdraw liquid products to compensate from the tank or for an increased amount of liquid product (s) to deliver. Depending on the amount of the second partial flow, there is a different amount in the work-related relaxation thereof Cold creates.

In jedem Fall können bei dem erfindungsgemäßen Verfahren sämtliche Ströme, die in die Rektifiziersäule(n) eingespeist oder daraus entnommen werden, konstant bleiben. Schwankungen in der Produktmenge haben damit keinerlei Auswirkungen auf die Rektifikation. Insbesondere können in jedem betriebsfall gleichbleibend hohe Reinheiten und Ausbeuten erzielt werden.In any case, in the method according to the invention, all of the streams that enter the rectification column (s) fed in or taken from it, remain constant. There are fluctuations in the product quantity no effects on rectification. In particular, consistently high purities can be achieved in every operating case and yields can be achieved.

Falls das Rektifiziersystem eine aus Drucksäule und Niederdrucksäule bestehende Doppelsäule aufweist, kann beispielsweise flüssiger Sauerstoff vom Sumpf der Niederdrucksäule oder verflüssigter Stickstoff aus der Drucksäule als flüssige Fraktion verwendet werden.If the rectification system has a double column consisting of a pressure column and a low pressure column, can, for example, liquid oxygen from the bottom of the low pressure column or liquefied nitrogen from the pressure column be used as a liquid fraction.

In einer günstigen Ausführungsform wird weiterer Strom des Wärmeträgers arbeitsleistend entspannt. Dadurch kann einerseits zusätzlich Kälte in dem Kreislauf erzeugt werden, andererseits ist eine weitere Möglichkeit zur genaueren Anpassung der Kälteleistung an den momentanen Bedarf gegeben, die unabhängig von der Regelung des Kreislaufverdichters und des zweiten Teilstroms ist.In a favorable embodiment, further flow of the heat transfer medium is relaxed while performing work. Thereby On the one hand, additional cold can be generated in the circuit, on the other hand there is another possibility for given more precise adjustment of the cooling capacity to the current demand, regardless of the regulation of the Circuit compressor and the second partial flow.

Insbesondere kann die Menge des weiteren Stroms, die der arbeitsleistenden Entspannung zugeführt wird, bei erhöhtem Bedarf an gasförmigem Druckprodukt erniedrigt werden und damit ein Überschuß an Kälte mindestens teilweise kompensiert werden. Vorzugsweise führt die arbeitsleistende Entspannung des weiteren Stroms etwa von dem Eintrittsdruck des Kreislaufverdichters (unteres Niveau des Kältekreislaufs) auf etwa Atmosphärendruck und der arbeitsleistend entspannte weitere Strom wird als druckloses Gasprodukt abgezogen. Damit lassen sich auch Schwankungen der im Kreislauf zirkulierenden Gasmenge auffangen. Insbesondere kann beispielsweise bei der ersten Betriebsweise (konstanter Durchsatz am Kreislaufverdichter) eine Verringerung der Menge des zweiten Teilstroms durch eine entsprechende Erniedrigung der Menge des arbeitsleistend entspannten weiteren Stroms ausgeglichen werden. Bei der zweiten Betriebsweise (konstanter Durchsatz bei der arbeitsleistenden Entspannung des zweiten Teilstroms) kann zum Beispiel eine Erhöhung des Kreislaufverdichterdurchsatzes durch eine Veringerung der Gasmenge kompensiert werden, die als weiterer Strom den Kreislauf verläßt.In particular, the amount of additional current that is supplied to the work-relieving relaxation can can be reduced if there is an increased need for gaseous printed product and at least an excess of cold partially compensated. Preferably, the work-performing relaxation of the further current leads approximately to the inlet pressure of the circuit compressor (lower level of the refrigeration circuit) to about atmospheric pressure and the more power that is relaxed during work is drawn off as an unpressurized gas product. This also allows fluctuations the amount of gas circulating in the circuit. In particular, for example, in the first mode of operation (constant throughput at the circuit compressor) by reducing the amount of the second partial flow a corresponding reduction in the amount of work-relaxed additional current can be compensated. In the second mode of operation (constant throughput during the work relieving pressure of the second partial flow) For example, an increase in the circulation compressor throughput can be compensated for by a reduction in the amount of gas that leaves the cycle as another stream.

Grundsätzlich kann jeder in dem Verfahren verfügbare Prozeßstrom als Wärmeträger für den Kältekreislauf und die Verdampfung der flüssigen Fraktion verwendet werden, beispielsweise Luft oder auch ein anderes Sauerstoff-Stickstoff-Gemisch. Bevorzugt wird jedoch Stickstoff aus dem Rektifiziersystem als Wärmeträger eingesetzt, im Falle einer Doppelsäule beispielsweise gasförmiger Stickstoff, der am Kopf der Drucksäule anfällt. In der Regel wird der gesamte Kreislaufstickstoff in der Anlage selbst produziert. Zusätzlich kann jedoch eine Teilmenge des Wärmeträgers aus einer äußeren Quelle stammen, beispielsweise durch Einspeisung von Flüssigstickstoff aus einer anderen Anlage oder aus einem Tankwagen in den zweiten Speichertank.In principle, any process stream available in the process can act as a heat transfer medium for the refrigeration cycle and the evaporation of the liquid fraction can be used, for example air or another oxygen-nitrogen mixture. However, nitrogen from the rectification system is preferably used as the heat carrier, in the case a double column, for example gaseous nitrogen, which accumulates at the top of the pressure column. As a rule, the entire cycle nitrogen is produced in the plant itself. In addition, however, a subset of the heat transfer medium come from an external source, for example by feeding liquid nitrogen from another plant or from a tank truck to the second storage tank.

Wenn Stickstoff als Produkt gewonnen wird, kann somit der zweite Speichertank neben seiner Pufferwirkung für die variable Druckproduktgewinnung auch als Sicherheitsreserve (Backup) für einen zeitweisen Ausfall der Anlage und/oder als Puffer für Flüssigprodukt eingesetzt werden.If nitrogen is obtained as a product, the second storage tank can act in addition to its buffering effect for variable print product production also as a safety reserve (backup) for a temporary failure of the system and / or used as a buffer for liquid product.

Außerdem hat die Verwendung von Stickstoff als Wärmeträgerden Vorteil, daß Kältekreislauf und Druckproduktverdampfung keinerlei negative Auswirkungen auf die Rektifikation hat, wie es bei der Zuspeisung von gegen Druckprodukt verflüssigter Luft und bei der Einspeisung von gasförmiger Luft aus einer Entspannungsmaschine in eine Niederdrucksäule der Fall wäre. Die Rektifikation kann also bei dem erfindungsgemäßen Verfahren mit Einsatz von Stickstoff als Wärmeträger optimal gefahren werden. Das Verfahren ist damit auch für hohe Produktreinheiten und - ausbeuten geeignet, ebenso wie für die Gewinnung von Argon im Anschluß an die Luftzerlegung im engeren Sinne (z.B. an die Niederdrucksäule einer Doppelsäule angeschlossene Rohargonsäule).In addition, the use of nitrogen as a heat transfer medium has the advantage that the refrigeration cycle and evaporation of the printed product does not have any negative effects on the rectification, as is the case when feeding in against Print product liquefied air and when feeding gaseous air from a relaxation machine in a low pressure column would be the case. The rectification can thus be used in the method according to the invention optimally driven by nitrogen as a heat transfer medium. The process is therefore also for high product purities and - exploit suitable, as well as for the extraction of argon after the air separation in the narrower sense (e.g. raw argon column connected to the low pressure column of a double column).

Es ist günstig, wenn die Einsatzluft für das Rektifiziersystem in einem Hauptwärmetauschersystem abgekühlt wird, in dem auch die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt wird. Durch diese Integraton der Wärmeaustauschvorgänge können die Austauschverluste gering gehalten werden.It is advantageous if the feed air for the rectification system is cooled in a main heat exchanger system is also carried out in which the evaporation of the liquid fraction is carried out under increased pressure. Through this integration heat exchange processes, the exchange losses can be kept low.

Dies kann zum einen dadurch realisiert werden, daß das Hauptwärmetauschersystem einen Wärmetauscherblock aufweist, in dem sowohl die Abkühlung der Einsatzluft als auch die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt werden.On the one hand, this can be achieved in that the main heat exchanger system has a heat exchanger block has in which both the cooling of the feed air and the evaporation of the liquid fraction below increased pressure.

Apparativ weniger aufwendig ist es jedoch, wenn das Hauptwärmetauschersystem mehrere Waärmetauscherblöcke aufweist, insbesondere einen ersten und einen zweiten Wärmetauscherblock, wobei in dem ersten Wärmetauscherblock die Abkühlung der Einsatzluft und in dem zweiten Wärmetauscherblock die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt wird. In diesem Fall ist es günstig, wenn die beiden Wärmetauscherblöcke durch einen Ausgleichsstrom gekoppelt sind, der einem der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende entnommen und dem anderen der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende zugeführt wird.However, it is less expensive in terms of equipment if the main heat exchanger system has a plurality of heat exchanger blocks has, in particular a first and a second heat exchanger block, wherein in the first heat exchanger block the cooling of the feed air and in the second heat exchanger block the evaporation of the liquid Fraction is carried out under increased pressure. In this case it is convenient if the two heat exchanger blocks are coupled by a compensating current that one of the two heat exchanger blocks between the removed warm and cold end and the other of the two heat exchanger blocks between the warm and cold end is fed.

Die Erfindung betrifft außerdem eine Vorrichtung gemäß Anspruch 7.The invention also relates to a device according to claim 7.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand des Ausführungsbeispiels des Linde-VARIPOX®-Verfahrens (VARiable Internal Pressurization of OXygen) und derentsprechenden Anlage näher erläutert, die in den Zeichnungen schematisch dargestellt sind.The invention and further details of the invention are described below using the exemplary embodiment the Linde VARIPOX® process (VARiable Internal Pressurization of OXygen) and the corresponding system explained in more detail, which are shown schematically in the drawings.

Verdichtete und gereinigte Einsatzluft 10 wird unter einem Druck von 5 bis 10 bar, vorzugsweise 5,5 bis 6,5 bar im Wärmetauscher 11 abgekühlt, der mit dem Wärmetauscher 12 das Hauptwärmetauschersystem bildet. Über Leitung 13 wird sie bei etwa Taupunktstemperatur in eine Drucksäule 14 eingeleitet. Die Drucksäule gehört zu dem Rektifiziersystem, das außerdem eine Niederdrucksäule 15 aufweist, die bei einem Druck von 1,3 bis 2 bar, vorzugsweise 1,5 bis 1,7 bar betrieben wird. Drucksäule 14 und Niederdrucksäule 15 sind über einen Hauptkondensator 16 thermisch gekoppelt.Compressed and cleaned feed air 10 is under a pressure of 5 to 10 bar, preferably 5.5 to 6.5 bar cooled in the heat exchanger 11, which forms the main heat exchanger system with the heat exchanger 12. about Line 13, it is introduced into a pressure column 14 at about dew point temperature. The pressure column belongs to that Rectification system, which also has a low pressure column 15, preferably at a pressure of 1.3 to 2 bar 1.5 to 1.7 bar is operated. Pressure column 14 and low pressure column 15 are via a main condenser 16 thermally coupled.

Sumpfflüssigkeit 17 aus der Drucksäule 14 wird in einem Gegenströmer 18 gegen Produktströme der Niederdrucksäule unterkühlt und in die Niederdrucksäule 15 eingespeist (Leitung 19). Gasförmiger Stickstoff 20 vom Kopf der Drucksäule 14 wird im Hauptkondensator 16 gegen verdampfende Flüssigkeit im Sumpf der Niederdrucksäule 15 verflüssigt. Das Kondensat 21 wird zu einem Teil als Rücklauf auf die Drucksäule 14 aufgegeben (Leitu ng 22) und zu einem anderen Teil 23 nach Unterkühlung 18 in einen Abscheider 25 eingeführt (24). Die Niederdrucksäule 15 wird aus dem Abscheider 25 mit Rücklaufflüssigkeit versorgt (Leitung 26).Bottom liquid 17 from the pressure column 14 is in a counterflow 18 against product flows of the low pressure column supercooled and fed into the low pressure column 15 (line 19). Gaseous nitrogen 20 from the head the pressure column 14 is in the main condenser 16 against evaporating liquid in the sump of the low pressure column 15 liquefied. The condensate 21 is partly fed as a return to the pressure column 14 (line 22) and to another part 23 introduced after supercooling 18 in a separator 25 (24). The low pressure column 15 will from the separator 25 supplied with return liquid (line 26).

Niederdruckstickstoff 27 und unreiner Stickstoff 28 werden nach Entnahme aus der Niederdrucksäule 15 in den Wärmetauschern 18 und 11 auf etwa Umgebungstemperatur angewärmt. Der unreine Stickstoff 30 kann zur Regenerierung eines nicht dargestellten Molekularsiebs für die Luftreinigung eingesetzt werden; der Niederdruckstickstoff 29 wird entweder als Produkt abgeführt oder in einem Verdunstungskühler zur Abkühlung von Kühlwasser verwendet.Low pressure nitrogen 27 and impure nitrogen 28 are 15 in after removal from the low pressure column the heat exchangers 18 and 11 warmed to about ambient temperature. The impure nitrogen 30 can be used for regeneration a molecular sieve, not shown, can be used for air purification; the low pressure nitrogen 29 is either discharged as a product or used in an evaporative cooler to cool cooling water.

Sauerstoff wird als flüssige Fraktion über Leitung 31 aus dem Sumpf der Niederdrucksäule 15 abgezogen, unterkühlt (18) und in einen Fiüssigsauerstofftank (ersten Speichertank) 33 eingeführt (32). Der Flüssigsauerstofftank 33 steht vorzugsweise unter etwa Atmosphärendruck. Flüssiger Sauerstoff 34 aus dem ersten Speichertank 33 wird mittels einer Pumpe 35 auf einen erhöhten Druck von beispielsweise 5 bis 80 bar gebracht, je nach benötigtem Produktdruck . (Selbstverständlich sind auch andere Methoden zur Druckerhöhung in der flüssigen Phase anwendbar, beispielsweise durch Ausnutzung eines hydrostatischen Potentials oder durch Druckaufbauverdampfung an einem Speichertank.) Der flüssige Hochdrucksauerstoff 36 wird im Wärmetauscher 12 verdampft und als innenverdichtetes gasförmiges Produkt 37 abgezogen.Oxygen is withdrawn as a liquid fraction via line 31 from the bottom of the low-pressure column 15, supercooled (18) and introduced (32) into a liquid oxygen tank (first storage tank) 33. The liquid oxygen tank 33 is preferably at about atmospheric pressure. Liquid oxygen 34 from the first storage tank 33 is brought to an increased pressure of, for example, 5 to 80 bar by means of a pump 35, depending on what is required Product printing. (Of course, other methods for increasing the pressure in the liquid phase can also be used, for example by utilizing a hydrostatic potential or by pressure build-up evaporation on one Storage tank.) The liquid high pressure oxygen 36 is evaporated in the heat exchanger 12 and as internally compressed deducted gaseous product 37.

Der Teil des gasförmigen Stickstoffs aus der Drucksäule 14, der nicht dem Hauptkondensator 16 zugeführt wird, wird über die Leitungen 38, 39 und 40 durch den Wärmetauscher 11 abgezogen und als Wärmeträger einem Kältekreislauf zugeführt, der unter anderem einen zweistufigen Kreislaufverdichter 41, 42 und eine Entspannungsturbine 43 umfaßt. Im Kreislaufverdichter 41, 42 wird der Stickstoff von etwa Druckstufendruck auf einen Druck komprimiert, der einer Stickstoff-Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatu r des flüssigen Drucksauerstoffs 36 ist. Dieser Druck beträgt-je nach vorgegebenem Abgabedruck des Sauerstoffs - beispielsweise 15 bis 60 bar. Ein erster Teilstrom 45 des hochverdichteten Stickstoffs 44 wird gegen den verdampfenden Sauerstoff 36 mindestens teilweise, vorzugsweise vollständig oder im wesentlichen vollständig verflüssigt und in einen Abscheider 46 eingespeist.The part of the gaseous nitrogen from the pressure column 14 that is not fed to the main condenser 16 is withdrawn via lines 38, 39 and 40 through the heat exchanger 11 and one as a heat carrier Refrigeration circuit supplied, which, among other things, a two-stage circuit compressor 41, 42 and an expansion turbine 43 includes. In the circuit compressor 41, 42, the nitrogen is compressed from about pressure stage pressure to a pressure which corresponds to a nitrogen condensation temperature which is at least approximately equal to the evaporation temperature r of the liquid pressurized oxygen 36. This pressure is - depending on the given delivery pressure of the oxygen - For example 15 to 60 bar. A first partial flow 45 of the highly compressed nitrogen 44 is against the evaporating Oxygen 36 at least partially, preferably completely or substantially completely liquefied and fed into a separator 46.

Der zweite Teilstrom 59 des im Kreislaufverdichter komprimierten Stickstoffs wird bei dem hohen Druck und bei einer Temperatur, die zwischen den Temperaturen am warmen und am kalten Ende des Wärmetauschers 12 liegt, der Entspannungsturbine 43 zugeleitet und dort auf etwa Drucksäulendruck arbeitsleistend entspannt. Der entspannte zweite Teilstrom 60 wird zum einen Teil du rch Wärmetauscher 12 (über 61, 62), zum anderen Teil durch Wärmetauscher 11 (über 63, 64, 39, 40) zum Eintritt des Kreislaufverdichters 41, 42 zurückgeführt.The second partial flow 59 of the nitrogen compressed in the circuit compressor is at the high pressure and at a temperature that lies between the temperatures at the warm and cold ends of the heat exchanger 12, fed to the expansion turbine 43 and relaxed there while performing work at about pressure column pressure. The relaxed one second partial flow 60 becomes partly through heat exchanger 12 (via 61, 62), partly through heat exchanger 11 (via 63, 64, 39, 40) returned to the inlet of the circuit compressor 41, 42.

Flüssiger Stickstoff aus dem Abscheider 46 kann über Leitung 47 als Rücklauf auf die Drucksäule 14 aufgegeben und/oder über Leitung 48 in einen zweiten Speichertank (Flüssigstickstofftank 49) eingeführt werden, der unter einem Druck von beispielsweise 1 bis 5 bar, vorzugsweise unter etwa Atmosphärendruck steht. Der Tank kann außerdem gegebenenfalls von überschüssiger Flüssigkeit 50 aus dem Abscheider 25 gespeist werden, die nicht als Rücklauf für die Niederdrucksäule 15 benötigt wird. Bei Bedarf kann flüssiger Stickstoff mittels einer Pumpe 51 in den Abscheider 46 gedrückt werden (Leitung 52).Liquid nitrogen from the separator 46 can be fed as a return line to the pressure column 14 via line 47 and / or are introduced via line 48 into a second storage tank (liquid nitrogen tank 49) which is under a pressure of, for example, 1 to 5 bar, preferably below about atmospheric pressure. The tank can also if necessary, excess liquid 50 is fed from the separator 25, which is not used as a return is required for the low pressure column 15. If necessary, liquid nitrogen can be fed into the separator by means of a pump 51 46 are pressed (line 52).

Ein Teil des Stickstoffs 53 aus Leitung 39 kann bei einer Zwischentemperatur aus dem Wärmetauscher 11 entnommen werden. Dieser Teil dient teilweise als Ausgleichsstrom 54, mit dessen Hilfe die Effizienz des Hauptwärmetauschersystems 11, 12 verbessert werden kann, und teilweise als weiterer Strom 55 des Wärmeträgers, der in einer zweiten Entspannungsturbine 56 arbeitsleistend auf etwas über Atmosphärendruck entspannt wird. Der arbeitsleistend entspannte weitere Strom 57 wird im Wärmetauscher 12 auf etwa Umgebungstemperatur angewärmt und verläßt die Anlage als gasförmiges Produkt 58.Part of the nitrogen 53 from line 39 can exit the heat exchanger 11 at an intermediate temperature be removed. This part serves in part as equalizing flow 54, with the aid of which the efficiency of the main heat exchanger system is increased 11, 12 can be improved, and in part as a further stream 55 of the heat carrier, which in a second expansion turbine 56 is expanded to work slightly above atmospheric pressure. The working relaxed further stream 57 is heated in the heat exchanger 12 to about ambient temperature and leaves the plant as a gaseous product 58.

Aus den Speichertanks 33, 49 können flüssiger Sauerstoff und/oder flüssiger Stickstoff als Produkte abgezogen werden (die entsprechenden Leitungen sind in der Zeichnung nicht dargestellt).Liquid oxygen and / or liquid nitrogen can be withdrawn as products from the storage tanks 33, 49 (the corresponding lines are not shown in the drawing).

Die Wechselspeicherung hat bei dem erfindungsgemäßen Verfahren keinerlei störende Einflüsse auf die Rektifikation, insbesondere wird weder Flüssigluft der Rektifikation zugeführt, noch wird Niederdruckluft direkt in die Niederdrucksäule eingespeist. Dadurch eignet sich der Prozeß hervorragend für besonders anspruchsvolle Trennaufgaben wie die Gewinnung von Argon. Dazu kann an einer Zwischenstelle 66 der Niederdrucksäule 15 eine konventionelle Argonrektifikation angeschlossen sein, wie es in der Zeichnung durch die dort gezeigten Leitungen angedeutet ist. Bevorzugt wird dazu einer der in EP-B-377117 oder in einer der europäischen Patentanmeldungen 95101844.9 oder 95101845.6 mit älterem Zeitrang beschriebenen Verfahren und Vorrichtungen eingesetzt.In the method according to the invention, the alternating storage has no disruptive influences on the rectification, in particular, neither liquid air is fed to the rectification nor is low-pressure air directly into the low-pressure column fed. This makes the process ideal for particularly demanding separation tasks like the production of argon. For this purpose, a conventional one can be located at an intermediate point 66 of the low-pressure column 15 Argon rectification connected, as indicated in the drawing by the lines shown there. For this purpose, one of the ones in EP-B-377117 or in one of the European patent applications 95101844.9 or is preferred 95101845.6 used methods and devices described with older seniority.

In dem Beispiel wird die erste Stufe 41 des Kreislaufverdichters auch als Produktverdichter verwendet, indem zwischen der ersten und der zweiten Stufe ein Produktstrom 65 unter einem Druck von vorzugsweise 8 bis 35 bar, beispielsweise 20 bar abgezogen wird.In the example, the first stage 41 of the cycle compressor is also used as a product compressor by between the first and the second stage a product stream 65 under a pressure of preferably 8 to 35 bar, for example, 20 bar is withdrawn.

Im folgenden werden nun die beiden grundsätzlichen Betriebsweisen eines Verfahrens und einer Vorrichtung gemäß der Erfindung erläutert. Die Anlage ist für eine bestimmte mittlere Menge an Drucksauerstoffprodukt ausgelegt. Die Produktion kann um diesen mittleren Wert schwanken, und zwarzwischen einem minimalen und einem maximalen Wert. Zur Erläuterung, wie diese Schwankung bewerkstelligt wird, werden in den folgenden Zahlenbeispielen die beiden extremen Betriebsfälle ("Max.", "Min.") und der Betriebsfall der durchschnittlichen Drucksauerstoffproduktion ("Mittl.") einer Anlage vorgestellt, die 190.000 Nm3/h Einsatzluft verarbeitet. Die Drücke betragen dabei Drucksäule 14 5,1 bar Niederdrucksäule 15 1,3 bar Drucksauerstoff 37 26 bar Eintritt des Kreislaufverdichters 4,8 bar Austritt des Kreislaufverdichters 42 bar Flüssigsauerstofftank 33 1,1 bar Flüssigstickstofftank 1,1 bar The two basic operating modes of a method and a device according to the invention are now explained below. The system is designed for a certain average amount of pressurized oxygen product. Production can fluctuate around this average value, and between a minimum and a maximum value. To explain how this fluctuation is achieved, the two extreme operating cases ("Max.", "Min.") And the operating case of the average pressure oxygen production ("Average") of a system are presented in the following numerical examples, the 190,000 Nm 3 / h Process air processed. The pressures are Pressure column 14 5.1 bar Low pressure column 15 1.3 bar Pressurized oxygen 37 26 bar Entry of the circuit compressor 4.8 bar Outlet of the circuit compressor 42 bar Liquid oxygen tank 33 1.1 bar Liquid nitrogen tank 1.1 bar

Tabelle 1 betrifft diejenige Betriebsweise, in der die Entspannungsturbine 43 für den zweiten Teilstrom 59 mit konstanter Drehzahl gefahren wird; bei der in Tabelle 2 dargestellten Betriebsweise wird der Durchsatz durch den Kreislaufverdichter 41, 42 konstant gehalten. Selbstverständlich ist auch bei dem Ausführungsbeispiel jeder beliebige Übergang zwischen diesen beiden Betriebsweisen möglich. In beiden Tabellen werden die Mengen der jeweiligen Ströme für die drei genannten Betriebsfälle in 1000 Nm3/h angegeben. Die Bezugszeichen in der ersten Tabellenspalte beziehen sich auf die Zeichnung. (Konstanter Durchsatz durch Turbine 43) Max. Mittl. Min. 50 Flüssigstickstoff aus dem Hauptkondensator zum Flüssigstickstofftank 1,5 1,5 1,5 32 Flüssiger Sauerstoff aus der Niederdrucksäule zum Flüssigsauerstofftank 36,5 36,5 36,5 40 Einspeisung von Drucksäulenstickstoff in den Kreislauf 90 90 90 53 Ausgleichsstrom + weiterer Strom (Turbine 56) 30 30 30 64 Entnahme von gasförmigem Stickstoff unter Drucksäulendruck aus dem Kreislauf 15 15 15 47 Flüssigstickstoff aus dem Flüssigstickstofftank und aus dem Kreislauf zum Kopf der Drucksäule 54 54 54 36 Zu verdampfender flüssiger Sauerstoff 45 35 25 37 Gasförmiges Druckprodukt (Sauerstoff) 45 35 25 44 Austritt des Kreislaufverdichters 93 83 73 45 Erster Teilstrom des Wärmeträgers 64 54 44 59
60 Zweiter Teilstrom des Wärmeträgers (Turbine 43) 28,5 28,5 28,5 61 Rückführung aus zweitem Teilstrom direkt durch Wärmetauscher 12 zum Kreislaufverdichter 13,5 13,5 13,5 54 Ausgleichsstrom 25 15 5 55
57 Weiterer Strom durch zweite Turbine 56 5 15 25 48 Flüssigstickstoff aus dem verflüssigten ersten Teilstrom in den Tank 10 0 0 52 Flüssigstickstoff aus dem Tank zur Drucksäule 0 0 10 65 Hochdruckstickstoffprodukt 35 35 35 (Konstanter Durchsatz durch Kreislaufverdichter 41, 42) Max. Mittl. Min. 50 Flüssigstickstoff aus dem Hauptkondensator zum Flüssigstickstofftank 1,5 1 ,5 1,5 32 Flüssiger Sauerstoff aus der Niederdrucksäule zum Flüssigsauerstofftank 36,5 36,5 36,5 40 Einspeisung von Drucksäulenstickstoff in den Kreislauf 90 90 90 53 Ausgleichsstrom + weiterer Strom (Turbine 56) 30 30 30 64 Entnahme von gasförmigem Stickstoff unter Drucksäulendruck aus dem Kreislauf 15 15 15 47 Flüssigstickstoff aus dem Flüssigstickstofftank und aus dem Kreislauf zum Kopf der Drucksäule 54 54 54 36 Zu verdampfender flüssiger Sauerstoff 45 35 25 37 Gasförmiges Druckprodukt (Sauerstoff) 45 35 25 44 Austritt des Kreislaufverdichters 83 83 83 45 Erster Teilstrom des Wärmeträgers 64 54 44 59
60 Zweiter Teilstrom des Wärmeträgers (Turbine 43) 18,5 28,5 38,5 61 Rückführung aus zweitem Teilstrom direkt durch Wärmetauscher 12 zum Kreislaufverdichter 3,5 13,5 23,5 54 Ausgleichsstrom 25 15 5 55
57 Weiterer Strom durch zweite Turbine 56 5 15 25 48 Flüssigstickstoff aus dem verflüssigten ersten Teilstrom in den Tank 10 0 0 52 Flüssigstickstoff aus dem Tank zur Drucksäule 0 0 10 65 Hochdruckstickstoffprodukt 35 35 35 Table 1 relates to the mode of operation in which the expansion turbine 43 for the second partial flow 59 is operated at a constant speed; in the operating mode shown in Table 2, the throughput through the circuit compressor 41, 42 is kept constant. Of course, any transition between these two modes of operation is also possible in the exemplary embodiment. In both tables, the amounts of the respective currents for the three operating cases mentioned are given in 1000 Nm 3 / h. The reference symbols in the first column of the table refer to the drawing. (Constant throughput by turbine 43) Max. Avg. Minute 50 Liquid nitrogen from the main condenser to the liquid nitrogen tank 1.5 1.5 1.5 32 Liquid oxygen from the low pressure column to the liquid oxygen tank 36.5 36.5 36.5 40 Feeding pressure column nitrogen into the circuit 90 90 90 53 Compensating current + additional current (turbine 56) 30 30 30 64 Removal of gaseous nitrogen from the circuit under pressure column pressure 15 15 15 47 Liquid nitrogen from the liquid nitrogen tank and from the circuit to the top of the pressure column 54 54 54 36 Liquid oxygen to be evaporated 45 35 25 37 Gaseous printed product (oxygen) 45 35 25 44 Outlet of the circuit compressor 93 83 73 45 First partial flow of the heat transfer medium 64 54 44 59
60 Second partial flow of the heat transfer medium (turbine 43) 28.5 28.5 28.5 61 Return from the second partial flow directly through heat exchanger 12 to the circuit compressor 13.5 13.5 13.5 54 transient 25 15 5 55
57 Further flow through second turbine 56 5 15 25 48 Liquid nitrogen from the liquefied first partial stream into the tank 10 0 0 52 Liquid nitrogen from the tank to the pressure column 0 0 10 65 High pressure nitrogen product 35 35 35 (Constant throughput by circuit compressors 41, 42) Max. Avg. Minute 50 Liquid nitrogen from the main condenser to the liquid nitrogen tank 1.5 1, 5 1.5 32 Liquid oxygen from the low pressure column to the liquid oxygen tank 36.5 36.5 36.5 40 Feeding pressure column nitrogen into the circuit 90 90 90 53 Compensating current + additional current (turbine 56) 30 30 30 64 Withdrawal of gaseous nitrogen under pressure from the circuit 15 15 15 47 Liquid nitrogen from the liquid nitrogen tank and from the circuit to the top of the pressure column 54 54 54 36 Liquid oxygen to be evaporated 45 35 25 37 Gaseous printed product (oxygen) 45 35 25 44 Outlet of the circuit compressor 83 83 83 45 First partial flow of the heat transfer medium 64 54 44 59
60 Second partial flow of the heat transfer medium (turbine 43) 18.5 28.5 38.5 61 Recirculation from the second partial flow directly through heat exchanger 12 to the circuit compressor 3.5 13.5 23.5 54 transient 25 15 5 55
57 Further flow through second turbine 56 5 15 25 48 Liquid nitrogen from the liquefied first partial stream into the tank 10 0 0 52 Liquid nitrogen from the tank to the pressure column 0 0 10 65 High pressure nitrogen product 35 35 35

Das Schema ist in der Zeichnung ist durch ein gestrichelte Linie in zwei Hälften geteilt. Die linke Hälfte enthält im wesentlichen den Kältekreislauf und die Speichertanks; die gesamte Rektifikation befindet sich in der rechten Hälfte. Im Wechselbetrieb des Verfahrens und der Anlage bleiben alle Ströme in der rechten Hälfte der Zeichnung vollständig oder im wesentlichen unverändert, die Schwankungen in der Drucksauerstoffproduktion wirken sich nur auf den Kreislauf und die Speichertanks aus. Dies spiegelt sich in den ersten sechs Zeilen der beiden Tabellen wieder, in denen sämtliche Ströme genannt sind, die die gestrichelte Linie überschreiten; diese weisen in allen Betriebsfällen den gleichen Durchsatz auf, während sich die Verdampfungsmenge ändert (Bezugszeichen 36, 37). Insbesondere wird über Leitung 38 eine konstante Menge von 105.000 Nm3/h Stickstoff aus der Drucksäule 14 in den variablen Teil der Anlage geführt, der in den Strömen 40 und 53 von einem - ebenfalls gleichbleibenden - Teil (15.000 Nm3/h) des in der Turbine 43 entspannten zweiten Teilstroms überlagert wird. Ebenso bleibt die Entnahme von flüssigem Sauerstoffprodukt 31, 32 aus der Niederdrucksäule 15 in allen Betriebsfällen konstant.The scheme in the drawing is divided in half by a dashed line. The left half essentially contains the refrigeration cycle and the storage tanks; the entire rectification is in the right half. In alternating operation of the process and the plant, all flows in the right half of the drawing remain completely or essentially unchanged, the fluctuations in the production of pressurized oxygen only affect the circuit and the storage tanks. This is reflected in the first six lines of the two tables, in which all currents are mentioned that cross the dashed line; these have the same throughput in all operating cases, while the amount of evaporation changes (reference symbols 36, 37). In particular, a constant amount of 105,000 Nm 3 / h of nitrogen is fed via line 38 from the pressure column 14 into the variable part of the system, which in the streams 40 and 53 consists of a - also constant - part (15,000 Nm 3 / h) of the in the turbine 43 relaxed second partial flow is superimposed. Likewise, the removal of liquid oxygen product 31, 32 from the low pressure column 15 remains constant in all operating cases.

In dem Zahlenbeispiel von Tabelle 1 wird der zweite Teilstrom 59, 60 konstant gehalten. Die für die Verdampfung notwendige Variation des ersten Teilstroms 45 wird durch die entsprechende Veränderung des Durchsatzes durch den Kreislaufverdichter (Strom 44) bewirkt: Erhöht sich beispielsweise die Produktion von dem durchschnittlichen auf den maximalen Wert, so nimmt der Durchsatz durch den Kreislaufverdichter etwa um denselben Betrag wie die Produktmenge zu. Das zusätzliche Gas wird durch eine entsprechende Verringerung der Gasmenge zur Verfügung gestellt, die als weiterer Strom 55, 57, 58 durch die Turbine 56 aus dem Kreislauf entnommen wird.In the numerical example in Table 1, the second partial flow 59, 60 is kept constant. The one for evaporation necessary variation of the first partial flow 45 is achieved by the corresponding change in the throughput the circulation compressor (stream 44) causes: For example, the production increases from the average the maximum value, the throughput through the circuit compressor increases by approximately the same amount as the product quantity to. The additional gas is made available by a corresponding reduction in the amount of gas, which is taken as a further stream 55, 57, 58 through the turbine 56 from the circuit.

Die schwankenden Mengen an verflüssigtem Wärmeträger (erster Teilstrom 45) werden dadurch gepuffert, daß bei überdurchschnittlicher Produktion über Leitung 48 überschüssige Flüssigkeit dem zweiten Speichertank 49 zugeführt wird; umgekehrt wird die fehlende Flüssigkeit bei geringer Produktmenge über Leitung 52 aus dem Flüssigstickstofftank nachgeführt, um die Rücklaufmenge für die Drucksäule 14 konstant zu halten.The fluctuating amounts of liquefied heat transfer medium (first partial flow 45) are buffered by that with above-average production via line 48 excess liquid to the second storage tank 49th is fed; conversely, the missing liquid is removed from the liquid nitrogen tank via line 52 with a small amount of product tracked to keep the return flow rate for the pressure column 14 constant.

Das Zahlenbeispiel von Tabelle 1 ist so ausgelegt, daß ein durchschnittlicher Überschuß an Flüssigkeit von jeweils 1500 Nm3/h Sauerstoff und Stickstoff erzeugt wird. Dieser kann kontinuierlich, intermittierend oder auch in variabler Menge in Form von Flüssigprodukten abgeführt werden. Im übrigen ist es bei dem Verfahren auch möglich, die durchschnittliche Kälteleistung des Kreislaufs und damit die mittlere Menge der Flüssigprodukte während des Betriebs zu verändern, indem die durchschnittlichen Drehzahlen der Turbinen entsprechend angepaßt werden. Die Anlage kann damit nicht nur bezüglich des innenverdichteten Druckprodukts, sondern auch hinsichtlich der Flüssigkeitsproduktion besonders flexibel betrieben werden.The numerical example of Table 1 is designed so that an average excess of liquid of 1500 Nm 3 / h oxygen and nitrogen is generated. This can be removed continuously, intermittently or in variable amounts in the form of liquid products. In addition, it is also possible with the method to change the average cooling capacity of the circuit and thus the average amount of liquid products during operation by adjusting the average speeds of the turbines accordingly. The system can be operated particularly flexibly not only with regard to the internally compressed printed product, but also with regard to liquid production.

Im Beispiel von Tabelle 2 wird statt des zweiten Teilstroms der Durchsatz des Kreislaufverdichters 41, 42 konstant gehalten.In the example in Table 2, the throughput of the circulation compressor 41, 42 is used instead of the second partial flow kept constant.

Claims (7)

  1. Process for the variable production of a gaseous pressurized product (37) by low-temperature separation of air, in which feed air (10, 13) is fed to a rectifying system (14, 15),
    a liquid fraction (31, 32, 34) from the rectifying system (14, 15) being buffered in a first reservoir tank (33),
    the pressure of the liquid fraction (34) being elevated (35) and
    a variable rate of the liquid fraction (36) being evaporated at the elevated pressure by indirect heat exchange (12) and obtained as gaseous pressurized product (37), in addition,
    a heat-transport medium being conducted in a refrigerating cycle which has a cycle compressor (41, 42),
    a first partial stream (44, 45) of the heat-transport medium compressed in the cycle compressor (41, 42) being fed to the indirect heat exchange (12) to evaporate the liquid fraction (36) and being, at least in part, liquefied,
    a second partial stream (44, 59) of heat-transport medium (44) compressed in the cycle compressor (41, 42) being expanded (43) so as to perform work and
    liquefied heat-transport medium (45, 48, 52) being buffered in a second reservoir tank (49), characterized in that a further stream (55) of the heat-transport medium is expanded (56) so as to perform work.
  2. Process according to Claim 1, characterized in that the rate of the further stream (55) which is fed to the work-performing expansion (56) is decreased when there is an increased demand for gaseous pressurized product (37).
  3. Process according to either of Claims 1 and 2, characterized in that nitrogen (31) from the rectifying system (14, 15) is used as heat-transport medium.
  4. Process according to one of Claims 1 to 3, characterized in that the feed air (10) for the rectifying system (14, 15) is cooled in a main heat exchanger system (11, 12), in which the evaporation (12) of the liquid fraction (36) at elevated pressure is also carried out.
  5. Process according to Claim 4, characterized in that the main heat exchanger system has a heat exchanger block in which both the cooling of the feed air and the evaporation of the liquid fraction at elevated pressure are carried out.
  6. Process according to Claim 4, characterized in that the main heat exchanger system has a first and a second heat exchanger block, in the first heat exchanger block (11) the cooling of the feed air (10) being carried out and in the second heat exchanger block (12) the evaporation of the liquid fraction (36) under elevated pressure being carried out, and the two heat exchanger blocks (11, 12) being coupled by a balance stream (54) which is taken off from one (11) of the two heat exchanger blocks between the hot and cold ends and is fed to the other (12) of the two heat exchanger blocks between the hot and cold ends.
  7. Apparatus for the variable production of a gaseous pressurized product by low-temperature separation of air,
    having a rectifying system (14, 15), into which leads a feed air line (10, 13),
    having a liquid line (31, 32) for the withdrawal of a liquid fraction from the rectifying system (14, 15) and for its introduction into a first reservoir tank (33),
    having means (35) for elevating the pressure of the liquid fraction (34),
    having a heat exchanger (12) for evaporating the liquid fraction (36) at elevated pressure,
    having a product line (37) for the withdrawal of the evaporated liquid fraction as gaseous pressurized product,
    having a refrigeration cycle, which has a cycle compressor (41, 42),
    having a first partial stream line (44, 45), which is connected from the cycle compressor (41, 42) to the heat exchanger (12) to evaporate the liquid fraction (36) ,
    having a second partial stream line (44, 59), which leads from the cycle compressor (41, 42) to an expansion engine (43) and
    having a second reservoir tank (49) for buffering liquefied heat-transport medium (45, 48), characterized by
    a third partial stream line (55), which leads from the cycle compressor (41, 42) to a further expansion engine (56).
EP96927545A 1995-07-21 1996-07-18 Method and device for the production of variable amounts of a pressurized gaseous product Expired - Lifetime EP0842385B2 (en)

Applications Claiming Priority (3)

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DE19526785 1995-07-21
DE19526785A DE19526785C1 (en) 1995-07-21 1995-07-21 Method and device for the variable production of a gaseous printed product
PCT/EP1996/003175 WO1997004279A1 (en) 1995-07-21 1996-07-18 Method and device for the production of variable amounts of a pressurized gaseous product

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EP0842385B1 EP0842385B1 (en) 2001-04-18
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EP2784420A1 (en) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Method for air separation and air separation plant
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DE102013017590A1 (en) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer
EP2963370B1 (en) 2014-07-05 2018-06-13 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
EP2963367A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for cryogenic air separation with variable power consumption
EP2963369B1 (en) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
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EP0842385B1 (en) 2001-04-18
JPH11509615A (en) 1999-08-24
KR100421071B1 (en) 2004-04-17
MX9800557A (en) 1998-04-30
ZA966146B (en) 1997-02-04
CA2227050A1 (en) 1997-02-06
DK0842385T3 (en) 2001-08-06
BR9609781A (en) 1999-12-21
ES2158336T3 (en) 2001-09-01
AU719608B2 (en) 2000-05-11
US5953937A (en) 1999-09-21
DE59606808D1 (en) 2001-05-23
CN1191600A (en) 1998-08-26
TW318882B (en) 1997-11-01
WO1997004279A1 (en) 1997-02-06
DE19526785C1 (en) 1997-02-20
CN1134638C (en) 2004-01-14
KR19990035798A (en) 1999-05-25
JP3947565B2 (en) 2007-07-25
AU6734496A (en) 1997-02-18
ES2158336T5 (en) 2004-07-01
DK0842385T4 (en) 2004-03-22
EP0842385A1 (en) 1998-05-20

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